EP0045853B1 - Oxidationskatalysator insbesondere für die Herstellung von Methacrylsäure durch Gasphasenoxidation von Methacrolein - Google Patents

Oxidationskatalysator insbesondere für die Herstellung von Methacrylsäure durch Gasphasenoxidation von Methacrolein Download PDF

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Publication number
EP0045853B1
EP0045853B1 EP81105341A EP81105341A EP0045853B1 EP 0045853 B1 EP0045853 B1 EP 0045853B1 EP 81105341 A EP81105341 A EP 81105341A EP 81105341 A EP81105341 A EP 81105341A EP 0045853 B1 EP0045853 B1 EP 0045853B1
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EP
European Patent Office
Prior art keywords
methacrolein
catalyst
oxidation
methacrylic acid
mol
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP81105341A
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German (de)
English (en)
French (fr)
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EP0045853A1 (de
Inventor
Richard Dr. Krabetz
Franz Dr. Merger
Matthias Dr. Schwarzmann
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BASF SE
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BASF SE
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Publication of EP0045853A1 publication Critical patent/EP0045853A1/de
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/85—Chromium, molybdenum or tungsten
    • B01J23/88—Molybdenum
    • B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8877—Vanadium, tantalum, niobium or polonium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8993—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with chromium, molybdenum or tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J27/195—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with vanadium, niobium or tantalum
    • B01J27/198—Vanadium
    • B01J27/199—Vanadium with chromium, molybdenum, tungsten or polonium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
    • C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

Definitions

  • catalysts which additionally contain other metals in addition to molybdenum, phosphorus and alkali metals or thallium are proposed as catalysts. From Japanese patent publication 68 122/1977, for example, catalysts are known which additionally contain niobium or vanadium and one or more elements from the group Mn, Sb, V, Fe, Cu, Ni, Si. However, these catalysts require bath temperatures above 330 ° C and therefore have a short lifespan.
  • Japanese patent publication 122317/1977 recommends catalysts which contain rhodium, metals from the group V, Cr, Fe and metals from the group Se, Ti, Sn, W, Al, Th as additional elements. With these catalysts, selectivities of 87.7 mol.% Are initially and briefly achieved at bath temperatures below 300.degree. However, it was found that the selectivity and activity decrease with the deformation of the catalyst mass necessary for industrial use and that the catalyst is sensitive to fluctuations in the operating conditions, so that the service life, particularly in the case of conversions above 70 mol%, leaves something to be desired.
  • a particular disadvantage of the catalyst systems known hitherto is that their performance drops considerably when technical methacrolein is used, which is produced by condensation of propionaldehyde with formaldehyde or aminals and which contains impurities, such as organic amines, dimers of methacrolein and methylpentenal, in a low concentration .
  • the catalyst can contain, among other things, vanadium, as component Y, among other things, cesium. The activity and selectivity of such catalysts still leaves something to be desired.
  • the catalysts of the invention are particularly suitable for the reaction of methacrolein, which is obtained by condensation of propionaldehyde and formaldehyde or aminals, since they are relatively insensitive to impurities in methacrolein such as amines, dimers of methacrolein and methylpentenal. Even with technical methacrolein grades, they achieve selectivities between 80 and 90 mol% at conversions above 60 mol% and reaction temperatures below 330 ° C, although no decrease in activity can be observed even after operating times of over 1,000 hours.
  • a further advantage of the catalysts according to the invention is the good deformability of the catalyst mass without appreciable impairment of the catalytic properties. In some cases, an improvement in the catalytic properties due to the deformation of the catalyst mass can even be observed.
  • the new catalysts can be produced, shaped and, if necessary, applied to supports in various ways.
  • a simple method of preparation is that the salts or oxides of the components are mixed in aqueous solution or suspension, then dried at temperatures between 70 and 130 ° C and finally calcined at temperatures between 180 and 600 ° C. It can be advantageous and is therefore preferred that the catalyst mass, if necessary after a relatively low temperature.
  • the catalyst can be with or without conventional carriers, such as silica, Ai 2 0 3, metal silicates, Ti0 2, Zr0 2 or pumice mixed can be used.
  • the deformation can be carried out before or after the activating calcination.
  • lubricants e.g. B. graphite powder
  • a (rather harmful) moistening of the powder to be tabletted is generally not necessary.
  • the catalyst mass can also be deformed into spheres by metering in the catalyst powder and a liquid binder, in a known ratio, in a certain quantity ratio, to preformed catalyst nuclei which roll in a turntable or a rotating inclined mixer.
  • a preferred method of shaping is that the catalyst powder is fed at a constant metering rate to a preformed inert carrier which is moved in a rotating container and continuously moistened with a liquid, wetting binder. Water is preferred as the binder.
  • Suitable carriers are spherically preformed A1 2 0 3 and magnesium aluminum silicate as well as conventional ceramic materials with particle diameters of 1.5-5 mm.
  • the amount of active composition on the carrier is generally 20-250% by weight, based on the carrier weight. Amounts of 50 to 200% by weight, based on the carrier weight, are preferred.
  • the process according to the invention is generally carried out at pressures between 1 and 5 bar and at temperatures between 200 and 400 ° C. advantageously at temperatures from 250 ° C. to 330 ° C.
  • the residence times are between 0.5 and 10 seconds, advantageously between 1 and 6 seconds.
  • Air is generally used as the oxidizing agent, but the oxygen can also be used in another form, e.g. B. be supplied as pure oxygen to the reactor.
  • the oxidation is advantageously carried out in the presence of inert gases, in particular water vapor.
  • the water vapor can be replaced in part by the reaction exhaust gas which, after washing and / or condensation of the products, is returned to the synthesis and generally consists of unreacted oxygen, nitrogen, carbon oxides and unreacted methacrolein and is saturated with water vapor according to the separation conditions.
  • the molar ratio of methacrolein: O 2 : H 2 0: inert gases is generally 1: 1-6: 1-20: 4-50, preferably 1: 1.5-4: 2-10: 6-30.
  • the methacrolein used can be prepared by various methods, e.g. B. by gas phase oxidation of tert. Butyl alcohol, isobutylene or C 4 mixtures or by condensation of propionaldehyde with formaldehyde.
  • Technical methacrolein is preferably used, which was obtained by condensation of propionaldehyde with formaldehyde in the presence of salts, sec-amines or with aminals in the presence of acids in aqueous solution.
  • Technical qualities generally have a degree of purity of 94-98% and contain, in addition to unreacted propionaldehyde, small amounts of organic amines, such as diethylamine or diethanolamine, methylpentenal and dimers of methacrolein. Due to the recycling of the unreacted methacrolein, the synthesis gas mixture can also contain small amounts of more volatile by-products of the process according to the invention.
  • the purity data relate to anhydrous raw methacrolein, in general the technical methacrolein contains up to 3.5% by weight of water.
  • the conversion of methacrolein can be carried out in fluidized bed reactors. However, it is preferred to work in so-called tube bundle reactors on fixed-bed catalysts. To avoid local overheating, the catalyst activity can be changed so that it rises steadily or in stages in the flow tube in the direction of flow. Suitable measures are, for example, dilution of the shaped catalyst with a few active or inactive catalyst or support moldings or the use of two or more catalysts with different activity and / or selectivity.
  • the methacrylic acid can be isolated from the reaction gases in a conventional manner.
  • the reaction offgas is cooled indirectly or directly and washed with water.
  • the methacrylic acid and, if appropriate, vinegar, maleic and acrylic acid can be extracted with suitable solvents, such as methyl methacrylate, and either fed directly to esterification with alkanols or separated by distillation from the extractant and the by-products.
  • suitable solvents such as methyl methacrylate
  • the catalysts of the invention also show in other oxidation processes, e.g. B. the oxidation of acrolein to acrylic acid or the oxidation of substituted toluene derivatives to substituted benzaldehydes and benzoic acids good effectiveness and selectivity.
  • methacrolein with a purity of 95 to 98% by weight is used which, in addition to propionaldehyde, contains small amounts of sec. Contained amines and by-products of methacrolein synthesis based on propionaldehyde / formaldehyde.
  • the catalyst A obtained has the composition Mo 12 V 1 P 1.96 Nb 0.53 Cs 1.95 Cu 0.5 Rh 0.1 O x
  • the bath temperature is slowly increased to 314 ° C.
  • the methacrolein conversion is 73.8 mol%
  • the yield of methacrylic acid is 66.5 mol%
  • the selectivity is 90.1 mol%.
  • the yields of by-products are 1.7 mol% of acetic acid, about 0.1 mol% of acrylic acid, about 0.4 mol% of maleic acid, about 0.4 mol% of other by-products, such as formaldehyde, acrolein, acetone, Acetaldehyde, benzaldehyde, formic acid and 4.8 mol% carbon oxides. If a quantity of catalyst of 50 ml is used and the bath temperature is increased to 320 ° C., the conversion is 60.6% and the selectivity is 88.1 mol%.
  • a catalyst B is produced as described in Example 1 with the difference that no Nb 2 0 3 is added. At a bath temperature of 300 ° C., a conversion of 80.6 mol%, a yield of methacrylic acid of 70 mol% and a methacrylic acid selectivity of 86.8 mol% is then achieved after 240 operating hours under example 1 under conditions specified in B. .
  • Example 1 a catalyst of the composition Mo 12 V 1 P 1 Cs 1 Cu 0.5 Nb 1 Rh 0.1 O x is produced and tested as indicated in Example 1B.
  • a bath temperature of 300 ° C a conversion of 77.9 mol% and a selectivity of methacrylic acid formation of 81.9 mol% is achieved.
  • the conversion is 88.1 mol.%
  • the selectivity of the acrylic acid formation is 80.2 mol.%.
  • Example 3 Catalysts are produced in accordance with Example 3, with the difference that one of the components Cu, Rh, V is omitted in each case.
  • the composition and test results under the conditions of Example 1B are summarized in Table 1 below.
  • the oxide mass obtained is reduced to a particle size of less than 50 ⁇ m.
  • 150 parts of the powder obtained are applied to 145 parts of steatite balls with a diameter of 3 mm in such a way that the powder is metered in at a constant metering rate to the carrier, which is continuously moistened with water and strongly agitated in a coating drum. After drying in the coating drum at 70 ° C with 100 ° C hot air, an abrasion-resistant coated catalyst is obtained.
  • Example 1A catalysts with different proportions of rhodium, copper and phosphorus are produced and tested under the conditions of Example 1A.
  • the test results are summarized in Table 2 below.
  • a catalyst of the composition Mo 12 V 1 P 1.96 Nb 0.53 Cs 1.95 Cu 0.05 Rh 0.1 O x was produced in accordance with the procedure of Example 1. 85 ml of the catalyst were, as indicated in Example 1B, heated to a bath temperature of 318 ° C. and tested with the bath temperature kept constant for 1 010 hours. The test results after various operating times are summarized in Table 3 below. No decline in turnover and selectivity can be observed within the test period.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
EP81105341A 1980-08-09 1981-07-09 Oxidationskatalysator insbesondere für die Herstellung von Methacrylsäure durch Gasphasenoxidation von Methacrolein Expired EP0045853B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19803030243 DE3030243A1 (de) 1980-08-09 1980-08-09 Oxidationskatalysator insbesondere fuer die herstellung von methacrylsaeure durch gasphasenoxidation von methacrolein
DE3030243 1980-08-09

Publications (2)

Publication Number Publication Date
EP0045853A1 EP0045853A1 (de) 1982-02-17
EP0045853B1 true EP0045853B1 (de) 1984-05-02

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Family Applications (1)

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EP81105341A Expired EP0045853B1 (de) 1980-08-09 1981-07-09 Oxidationskatalysator insbesondere für die Herstellung von Methacrylsäure durch Gasphasenoxidation von Methacrolein

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US (2) US4409128A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
EP (1) EP0045853B1 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
JP (1) JPS5759639A (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)
DE (2) DE3030243A1 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html)

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59115750A (ja) * 1982-12-22 1984-07-04 Nippon Shokubai Kagaku Kogyo Co Ltd メタクリル酸合成用触媒
JPS6056389A (ja) * 1983-09-08 1985-04-01 松下電器産業株式会社 長尺ヒ−タの製造方法
JPS6081786A (ja) * 1983-10-07 1985-05-09 松下電器産業株式会社 長尺ヒ−タ
GB2171925B (en) * 1985-02-02 1988-10-19 Agency Ind Science Techn Process for the manufacture of ethanol based, oxygen-containing carbon compounds
JPH0813778B2 (ja) * 1988-07-11 1996-02-14 住友化学工業株式会社 メタクリル酸の製造方法
US5239105A (en) * 1992-01-30 1993-08-24 The Dow Chemical Company Catalytic formation of diarylcarbonates
US6432870B1 (en) * 1999-05-25 2002-08-13 Toagosei Co., Ltd. Process for preparing metal oxide catalyst for acrylic acid production
JP3702710B2 (ja) * 1999-06-15 2005-10-05 住友化学株式会社 メタクリル酸製造用触媒およびメタクリル酸の製造方法
DE102012207811A1 (de) 2012-05-10 2012-07-12 Basf Se Verfahren der heterogen katalysierten Gasphasenpartialoxidation von (Meth)acrolein zu (Meth)acrylsäure
WO2014146961A1 (en) 2013-03-18 2014-09-25 Evonik Industries Ag Process for preparation of methacrylic acid and methacrylic acid esters

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2460541C3 (de) * 1973-12-29 1979-10-18 Nippon Shokubai Kagaku Kogyo Co. Ltd., Osaka (Japan) Phosphor, Molybdän und Vanadium sowie gegebenenfalls Kupfer, Kobalt, Zirkon, Wismut, Antimon und/oder Arsen enthaltender Oxydkatalysator und dessen Verwendung zur Herstellung von Methacrylsäure
US4049574A (en) * 1974-05-28 1977-09-20 Petro-Tex Chemical Corporation Catalyst and process for preparing maleic anhydride from C4 hydrocarbons
JPS5827255B2 (ja) 1974-05-31 1983-06-08 三菱レイヨン株式会社 不飽和脂肪酸の製造方法
US4017423A (en) * 1975-08-18 1977-04-12 The Standard Oil Company (Ohio) Process for the preparation of unsaturated acids from unsaturated aldehydes
US4075124A (en) * 1976-10-19 1978-02-21 The Standard Oil Company Process for the preparation of unsaturated acids from unsaturated aldehydes
US4202826A (en) * 1977-02-10 1980-05-13 Denka Chemical Corporation Process for preparing anhydride from alkanes
JPS6048496B2 (ja) * 1977-07-22 1985-10-28 東ソー株式会社 メタクリル酸の製造方法
JPS5924140B2 (ja) * 1977-10-31 1984-06-07 日本化薬株式会社 メタクリル酸の製造法及び触媒
DE2962547D1 (en) * 1978-05-31 1982-06-03 Nippon Kayaku Kk A process for producing methacrolein and methacrylic acid
NL7909142A (nl) * 1978-12-26 1980-06-30 Halcon Res & Dev Katalysator en werkwijze voor de bereiding van methacrylzuur.
YU41495B (en) * 1979-01-23 1987-08-31 Nippon Kayaku Kk Process for obtaining methacrolein and methacrylic acid
US4280928A (en) * 1979-10-12 1981-07-28 Rohm And Haas Company Catalyst compositions and their use for the preparation of methacrolein
US4301031A (en) * 1980-08-05 1981-11-17 The Standard Oil Company Methacrolein oxidation catalysts

Also Published As

Publication number Publication date
JPS5759639A (en) 1982-04-10
EP0045853A1 (de) 1982-02-17
JPH0211307B2 (GUID-C5D7CC26-194C-43D0-91A1-9AE8C70A9BFF.html) 1990-03-13
US4487962A (en) 1984-12-11
DE3030243A1 (de) 1982-03-18
US4409128A (en) 1983-10-11
DE3163381D1 (en) 1984-06-07

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